Note : Les descriptions sont présentées dans la langue officielle dans laquelle elles ont été soumises.
IONIC LIQUID COMPOUND FOR CATALYSIS OF CHEMICAL REACTIONS
FIELD
The present disclosure relates to an ionic liquid compound and its
preparation. The
present disclosure also relates to the use of ionic liquid compound for
catalysing the
chemical reactions.
BACKGROUND
Ionic liquids are liquids that are composed entirely of ions or a combination
of cations
and anions. The "low temperature" ionic liquids are generally organic salts
with
melting points less than 100 degrees C., often even lower than room
temperature.
Ionic liquids may be suitable, for example, for use as catalysts and solvents
in
alkylation and polymerization reactions as well as in dimerization,
oligomerization
acetylation, metatheses and copolymerization reactions.
One class of ionic liquids is fused salt compositions, which are molten at low
temperature and are useful as catalysts, solvents and electrolytes. Such
compositions
are mixtures of components which are liquids at temperatures below the
individual
melting points of the components.
Ionic liquids can be defined as liquids whose make-up entirely comprises ions
as a
combination of cations and anions. The most common ionic liquids are those
prepared
from organic-based cations and inorganic or organic anions. The most common
organic cations are ammonium cations, however phosphonium and sulphonium
cations are also frequently used. Ionic liquids of pyridinium and imidazolium
are
perhaps the most commonly used cations. Anions include, but are not limited to
BF4¨, PF6¨, haloaluminates such as Al2C17¨ and Al2Br7¨, [(CF3S02)2N)]¨, alkyl
sulphates (RS03¨), carboxylates (RCO2¨) and the like. The most catalytically
interesting ionic liquids are those derived from ammonium halides and Lewis
acids
(such as AlC13, TiC14, SnC14, FeC13 and the like). Chloroaluminate ionic
liquids are
perhaps the most commonly used ionic liquid catalyst systems.
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The alkylation of benzene with acyclic olefins is a widely practiced
commercial
process. This process is performed to produce a variety of chemical compounds
which
may be end products or may be used as intermediates in the production of other
valuable industrial chemicals. One of the most significant processes for the
alkylation
of aromatic hydrocarbons employs liquid phase HF as a catalyst and is
performed to
produce alkyl benzenes which are further converted into detergents by
sulfonation and
neutralization.
United States Patent No. 3249650 discloses the use of an HF catalyst for the
reaction
of isoparaffin and olefin. The reaction involves passing the iosparaffin-
olefin stream
in to an alkylation reactor along with an HF catalyst and continuously
withdrawing a
portion of hydrocarbon-HF mixture.
United States Patent No. 3494971 discloses alkylation of benzene with C10-C15
olefins
in two stages with hydrogen fluoride as a catalyst at 100 F temperature. The
HF
catalyst employed in the first stage is a used catalyst and the HF used in the
second
stage is a fresh or regenerated catalyst.
United States Patent No. 3560587 discloses the use of hydrogen fluoride
catalyst for
the alkylation of isoparaffin with olefin. In the process, a mixture is passed
into a
reaction cooler equipped with an internally placed heat exchanger, wherein the
mixture is contacted with HF catalyst under isothermal reaction conditions and
the
reaction effluent is then passed into a reaction soaker equipped with a number
of
spaced perforated plates therein in which further alkylation takes place.
United States Patent No.3686354 discloses a method of producing high octane
paraffinic motor fuel by alkylating isobutene and a C4 mono olefin in the
presence of
hydrogen fluoride catalyst. United States Patent No. 3713615 discloses an
alkylation
fractionator having a settling section for separating liquid catalyst from the
effluent of
an alkylator. The lighter isoparaffins are stripped off from the heavier
fractions in a
fractionation section below the acid settling section.
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United States Patent No. 4239931 discloses hydrofluoric acid-catalyzed
alkylation of
an isobutane with a mixture of propylene and butylene at 200 T in an
isoparaffin
stripping column-integrated acid catalyst regeneration system.
United States Patent No. 3950448 discloses production of detergent grade
alkylate by
HF acid catalysed reaction of aromatic hydrocarbons and an olefinic
hydrocarbon. The
process describes the use of unique fractionation facility for the recovery
and use of an
aromatic concentrate and recovery of detergent alkylate product.
Use of Lewis acid catalysts has also been disclosed for alkylation. United
States
Patent No. 3104267 discloses a method of preparing alkyl aromatic hydrocarbons
by
contacting ethylene with benzene, toluene & xylene containing catalytic
mixture of
titanium tetrachloride and alkyl aluminium di ch loride/di al kyl aluminium
chloride/alkylaluminium sesquichloride, where the ethylene is polymerized to a
long
chain olefin without substantial reaction of said aromatic and then contacting
the
reaction mixture with dry HC1/HBr, whereby the said long chain olefin
alkylates to
aromatic hydrocarbon. The temperature range used was 100-400 T.
United States Patent No. 4219686 discloses a method of producing heavy alkyl
benzenes and linear dodecyl benzene comprising of two steps. Auto-condensation
of
C11 to C14 olefins in the presence of Aluminum chloride catalyst followed by
alkylation of benzene with the above reaction mixture in the presence of
aluminum
Chloride where the mixture is saturated with gaseous hydrogen chloride at 40-
42 C.
United States Patent No. 5284993 discloses a method of regeneration of
catalyst used
for alkylation of olefins by isoparaffins. The catalyst comprises of
fluorosulphonic
acid/triflouoromethanesulphonic acid and methanesulphonic acid. The process
mainly
describes the removal of acid soluble oils (ASO) produced as an undesirable by-
product during the reaction. The process includes the use of water to induce
the
formation of the two immiscible phases of ASO and methanesulphonic acid.
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US20100094072A1 discloses the use of a catalyst for the isoparaffin-olefin
alkylation.
The catalyst is obtained by admixing a trifluoromethanesulfonic acid on a
polyacrylic
acid support. It was also found that the use of solid catalysts facilitates
the production
of linear alkyl benzenes. United States Patent No.5334793 discloses the use of
HF
solid acid catalyst for the alkylation of benzene with olefin feed stock
obtained from
dehydrogenation unit containing linear paraffin having 8 to 16 carbon atoms.
United States Patent No. 7737312 discloses the use of UOP DETAL solid acid
catalyst for the production of linear alkyl benzene (LAB) from the olefin
stream
obtained from Fischer-Tropsch reaction. The above obtained stream is reacted
with
benzene to produce LAB.
Similarly, several other solid catalysts were reported so far for the
alkylation-leaction:
United, States Patent Nos. 3346657, US4358628, US4368342, US4513156,
US4973780, US5196574, US5196624, US5344997, US5574198, US 5777187,
US5847254, US5894076, US6133492, US7655824, US2011/0118517,
US20110144403.
Further, several ionic liquid catalysts were reported for alkylation reaction.
For
instance, W0/1998/003454 discloses the use of alkyl- containing amine
hydrohalide
ionic liquids for the reaction of benzene with an olefin having an average
carbon
content of over 10, a chloroalkane having an average carbon content of over 6,
or
mixture thereof.
United States Patent No. 5824832 dislcoses ionic liquids comprising a mixture
of a
metal halide and an alkyl-containing amine hydrohalide salt for the production
of
linear alkyl benzene. The metal halide is a covalantly bonded metal halide
which can
contain a metal selected from the group comprised of aluminum, gallium, iron,
copper, zinc and indium.
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WO/1999/003163 discloses alkylation of aromatic compounds using a catalyst
which
comprises a porous support impregnated with an ionic liquid consisting of an
organic
base and a metal. Organic base is selected from the group consisting of a
halide of
imidazolium, pyridinium, sulfonium, phosphonium, guanidinium, and ammonium and
metal halide is selected from the group comprised of aluminum, gallium, iron,
copper,
zinc, and indium. =
WO/2000/041809 discloses the use of catalyst comprising a pre-formed complex
of an
ionic liquid and an aromatic hydrocarbon for the alkylation of aromatic
hydrocarbons
with C2 to C10 olefin. The ionic liquid comprises a first component of the
formula
R0MX3, (wherein R is a C1-C6 alkyl group, M is aluminium or gallium, X is a
halogen atom) and a second component selected from the group consisting of an
alkyl
ammonium halide, an imidazolium halide, a pyridinium halide, a hydrocarbyl
substituted quaternary ammonium halide, a hydrocarbyl substituted quaternary
phosphonium halide and mixtures thereof.
United States Patent No. 7285698 discloses a method for alkylation of
isobutane and
C4 olefin using a composite ionic liquid as a catalyst. The ionic liquid
comprises a
cation which is a hydrohalide of an alkyl-containing amine or pyridine and an
anion
which is a mixture of aluminum halide and halides or sulphates or nitates of
copper,
iron, zinc, nickel, cobalt, molybdenum or platinum.
The ionic liquid catalysts as dislcoed in the prior art documents are found to
be less
effective when used in the alkylation reactions. Further, these known ionic
liquid
catalysts are expensive. Accordingly, there is felt a need for a cost-
effective ionic
liquid compound which can effectively catalyze Friedel crafts reactions such
as
alkylation reactions.
OBJECTS:
Some of the objects of the present disclosure, which at least one embodiment
herein
satisfies, are as follows:
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It is an object of the present disclosure to provide an ionic salt complex as
a precursor
of ionic liquid compound.
It is another object of the present disclosure to provide a simple and cost
effective
process for the preparation of ionic salt complex.
It is still another object of the present disclosure to provide a process for
the
preparation of ionic salt complex in the presence or absence of a solvent.
It is another object of the present disclosure to provide a cost-effective
ionic liquid
compound which can be used as a catalyst and/or solvent.
It is still another object of the present disclosure to provide a simple and
cost effective
process for the preparation of an ionic liquid compound.
It is yet another object of the present disclosure to provide a process for
the
preparation of an ionic liquid which can be carried out in the presence of a
solvent to
achieve the desired viscosity of the ionic liquid.
It is a further object of the present disclosure to provide an ionic liquid
catalyst which
can be used for Diels-Alder reaction, Friedel crafts reactions such as
alkylation,
acylation, alkyl-sulfonation, and the like.
It is still further object of the present disclosure to provide a recycled
ionic liquid
compound which can be used as a catalyst in an alkylation reaction.
It is another object of the present disclosure to provide an ionic liquid
catalysed Diels-
Alder reaction, Friedel crafts reactions such as alkylation, acylation, alkyl-
sulfonation,
and the like.
It is another object of the present disclosure to provide a simple and cost
effective
alkylation reaction using the ionic liquid compound.
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It is another object of the present disclosure to an alkylation reaction in
which the used
ionic liquid catalyst can be easily recovered and recycled.
Summary
The present disclosure provides an ionic liquid compound of Formula (I):
RNR1R2R3)Miin+i(M2YOL NJ'
Formula I
wherein,
NR1R2R3 represents an amine,
RI, R2 and R3 are independently selected from the group consisting of alkyl,
aryl and H,
M1 or M2 is a metal selected from the group consisting of Al, Fe, Zn, Mn and
Mg, Ti, Sn, Pd, Pt, Rh, Cu, Cr, Co, Ce, Ni, Ga, In, Sb, Zr and combinations
thereof,
X or Y is selected from the group consisting of halogen, nitrate, sulphate,
sulfonate, carbonate, phosphonate and acetate,
`11' represents 1 to 4,
i' represents 1 to 6,
j 'represents 1 to 4,
'k' represents 1 to 4,
`L' represents 1 to 7,
Mi = M2 or M1lV12, and
X = Y or X Y.
Typically, the alkyl group is selected from the group consisting of methyl,
ethyl,
propyl, butyl and combinations thereof; the aryl group is selected from the
group
consisting of benzyl, phenyl, substituted benzenes and combinations thereof;
and the
halogen is selected from the group consisting of F, Cl, Br and I.
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Typically, NR1R2R3 is a trialkylamine; MI or M2 is a metal selected from the
group
consisting of Al, Fe, Zn, Mn, Mg, Ti, Sn, Pd, Pt, Rh, Cu, Cr, Co, Ce, Ni, Ga,
In, Sb,
Zr and combinations thereof; and X or Y is a halogen.
In accordance with another aspect of the present disclosure there is provided
a process
for the preparation of an ionic liquid compound of Formula (I),
KNRIR2R0iMiri(M2Yk)L
Formula!
wherein,
NR1R2R3 represents an amine,
RI, R2 and R3 are independently selected from the group consisting of alkyl,
aryl and H,
M1 or M2 is a metal selected from the group consisting of Al, Fe, Zn, Mn and
Mg, Ti, Sn, Pd, Pt, Rh, Cu, Cr, Co, Ce, Ni, Ga, In, Sb, Zr and combinations
thereof,
X or Y is selected from the group consisting of halogen, nitrate, sulphate,
sulfonate, carbonate, phosphonate and acetate, 'n' represents 1 to 4,
i' represents 1 to 6,
`j 'represents I to 4,
'k' represents I to 4,
'1.,' represents 1 to 7,
Mi = M2 or M4M2, and
X = Y or X Y,
said process comprising the following steps:
i. preparing an ionic salt complex precursor represented by Formula
f(NRIR2R3),M1r[Xi] by mixing an amine represented by Formula NR1R2R3
and a metal salt represented by formula MIN; and
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ii. mixing the ionic salt complex precursor and a metal salt represented by
formula M2Yk to obtain the ionic liquid compound.
Typically, the step (i) is carried out at a temperature ranging from -20 to
100 C.
Typically, the step (i) is carried out in the presence of a solvent selected
from the
group consisting of ethyl acetate, ethanol, methanol, methyl iso butyl ketone,
methyl
ethyl ketone, benzene, toluene, dichloromethane and combinations thereof.
Typically, the step (ii) is carried out at a temperature ranging from -20 to
100 C.
Typically, the step (ii) is carried out in the presence of a solvent selected
from the
group consisting of methyl iso butyl ketone, methyl ethyl ketone, benzene,
toluene,
dichloromethane and combinations thereof.
Typically, the mole ratio of the amine to the metal salt ranges from 1:0.1 to
1:0.5.
Typically, the mole ratio of the ionic salt complex precursor to the metal
salt ranges
from 1:3 to 1:6.
Typically, ionic liquid compound is [(Et3N)3-A03+[(A1C13)6C13]3" prepared by
mixing
triethylamine and AlC13 to form ionic salt complex precursor, REt3N)3-
A03+[(C1)3}3- ;
and complexing said ionic salt complex precursor with AlC13.
In accordance with still another aspect of the present disclosure there is
provided an
ionic salt complex precursor represented by Formula (II)
[(NRIR2R3)iM1 rper
Formula II
wherein,
INTRIR2R3 represents an amine,
RI, R2 and R3 are independently selected from the group consisting of
alkyl, aryl and H,
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Mt or M2 is a metal selected from the group consisting of Al, Fe, Zn,
Mn and Mg, Ti, Sn, Pd, Pt, Rh, Cu, Cr, Co, Ce, Ni, Ga, In, Sb, Zr and
combinations thereof,
X or Y is selected from the group consisting of halogen, nitrate,
sulphate, sulfonate, carbonate, phosphonate and acetate,
'n' represents 1 to 4,
T represents 1 to 6, and
`j 'represents 1 to 4,
In accordance with yet another aspect of the present disclosure there is
provided a
process for preparing an ionic salt complex precursor represented by Formula
[(NR1R2R3),M1]"[Xj] comprises mixing an amine represented by Formula NRIR2R3
and a metal salt represented by formula MA.
Typically, the ionic salt complex precursor is [(Et3N)3-A1131(C1)3J3- prepared
by
mixing triethylamine and AlC13.
In accordance with a further aspect of the present disclosure there is
provided a
process for conducting at least one reaction selected from the group
consisting of
alkylation reaction, arylation reaction, acylation reaction, diels alder
reaction and
oligomerization reaction of at least one compound selected from the group
consisting
of CI to C20 aliphatic compounds, C6 to C8 aromatic compounds and heteroaryl
compounds in the presence of an ionic liquid compound represented by formula
RNIZIR2R3)Mir+RM2YOL Xir and at a temperature of 20 to 1000C,
wherein,
NR1R2R3 represents an amine,
RI, R2 and R3 are independently selected from the group consisting of alkyl, '
aryl and H,
M1 or M2 is a metal selected from the group consisting of Al, Fe, Zn, Mn and
Mg, Ti, Sn, Pd, Pt, Rh, Cu, Cr, Co, Ce, Ni, Ga, In, Sb, Zr and combinations
thereof,
X or Y is selected from the group consisting of halogen, nitrate, sulphate,
sulfonate, carbonate, phosphonate and acetate,
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'p' represents 1 to 4.
'V represents 1 to 6,
'represents 1 to 4,
'le represents 1 to 4,
`L' represents 1 to 7,
Mi --- M2 or I\AIIVI2, and
X = Y or X t Y.
Typically, said reaction is carried out using at least one reactant selected
from the
group consisting of olefins, paraffins, alkyl or aryl halides, dialkyl or
diary! sulfates,
dialkyl or diary! carbonates, alcohols, carboxylic acids, esters, thiols and
carbenes.
Typically, the reactant is olefin or a mixture of olefins having carbon atoms
ranging
from 2 to 50.
Typically, the volume ratio of ionic liquid compound to the compound ranges
from
0.01 to 1.5.
The process also includes a step of recovering and recycling of said ionic
liquid
compound.
Typically, said ionic liquid compound is selected from the group consisting of
fresh
ionic liquid compound, recycled ionic liquid compound and a combination
thereof
In one embodiment said reaction is an alkylation of benzene; said reaction
comprises
alkylating benzene at a temperature of 20 to 100 C, preferably at 30 to 60 C
in the
presence of an ionic liquid compound represented by formula
[(NRIR2R3);Mi]l(M2YOL Xir and at least one alkylating agent to obtain
linear alkyl benzene.
Typically, the alkylating agent is a mixture of at least one C2 to C50
containing olefin
and at least one C2 to C50 containing paraffin.
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Typically, the alkylating agent is olefin selected from the group consisting
of C10 to
C14 olefins and mixtures thereof.
Typically, the ratio of benzene to the alkylating agent ranges from 1:1 to
20:1,
preferably, 6:1 to 10:1.
Typically, the alkylation of benzene is carried out at a pressure ranging from
1 to 10
atmospheres, preferably 1 to 6 atmospheres.
BRIEF DESCRIPTION OF THE ACCOMPANYING DRAWINGS: -
FIGURE 1 illustrates a process flow diagram for the preparation of the ionic
salt
complex precursor;
FIGURE 2 of the accompanying drawings illustrates a process flow diagram for
the
preparation of the ionic liquid compound; and
FIGURE 3 illustrates alkylation process using the ionic liquid compound of the
present disclosure.
DETAILED DESCRIPTION:
The present disclosure provides an ionic liquid compound which can be
effectively
used as a catalyst and/or solvent to catalyse the Diels-Alder reaction,
Friedel crafts
reactions such as alkylation, acylation, alkyl-sulfonation and the like.
The ionic liquid compound of the present disclosure is represented by Formula
(I)
{(NRIR2R3)1Mir[(M2YOL X]
Formula I
In accordance with the present disclosure, NR1R2R3 represents an amine in
which RI,
R2 and R3 are either alkyl group or aryl group or H .i.e. amine is either
alkyl amine or
aryl amine. The alkyl group includes but is not limited to methyl, ethyl,
propyl, butyl
and combinations thereof. The aryl group is selected from the group consisting
of
benzyl, phenyl, substituted benzenes and combinations thereof.
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M1 or M2 is a metal selected from the group consisting of Al, Fe, Zn, Mn, Mg,
Ti, Sn,
Pd, Pt, Rh, Cu, Cr, Co, Ce, Ni, Ga, In, Sb, Zr and combinations thereof.
In accordance with the present disclosure, X or Y is selected from the group
consisting of halogen, nitrate, sulphate, sulfonate, carbonate, phosphonate
and acetate.
In accordance with the present disclosure the halogen is selected from the
group
consisting of F, Cl, Br and I.
In the formula I,
'n' represents 1 to 4,
`i' represents 1 to 6,
`j 'represents 1 to 4,
'k' represents 1 to 4,
`L' represents 1 to 7,
Mi = M2 or Nl1M2, and
X Y or X Y.
In one embodiment NR1R2R3 is a trialkylamine, M1 or M2 is a metal selected
from the
group consisting of Al, Fe, Zn, Mn and Mg, Ti, Sn, Pd, Pt, Rh, Cu, Cr, Co, Ce,
Ni, Ga,
In, Sb, Zr and combinations thereof and X or Y is a halogen.
In one exemplary embodiment the ionic liquid compound is [(Et3N)3-
Alf+RAICI3)6C1313'.
In accordance with another aspect of the present disclosure there is provided
a process
for the preparation of an ionic liquid compound of Formula (I),
[(NR1R2RAM ]"[(1\42YOL Xyr
The process involves the following steps:
In the first step an ionic salt complex, represented by Formula
[(NRIR2R3)1M1]0riXj1,
is prepared by mixing an amine, represented by Formula NR1R2R3 and a metal
salt
represented by formula MIN.
This first step is carried out at a temperature ranging from -20 to 100 C and
in the
absence or presence a solvent. The solvent includes but is not limited to
ethyl acetate,
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ethanol, methanol, methyl iso butyl ketone, methyl ethyl ketone, benzene,
toluene,
dichloromethane and combinations thereof.
In accordance with the present disclosure the mole ratio of the amine to the
metal salt
is maintained in the range from 1:0.1 to 1:0.5.
In the second step, the ionic salt complex and a metal salt represented by
formula
M2Yk are mixed to obtain the ionic liquid compound. The mole ratio of the
ionic salt
complex to the metal salt is maintained in the range from 1:3 to 1:6. The
second step
is carried out at a temperature ranging from -20 to 100 C in the absence or
presence of
a solvent. The solvent includes but is not limited to ethyl acetate, ethanol,
methanol,
methyl iso butyl ketone, methyl ethyl ketone, benzene, toluene,
dichloromethane and
combinations thereof.
The complex (ionic liquid compound) formed by reacting ionic salt complex and
a
metal salt is either eutectic or non-eutectic.
In one exemplary embodiment the ionic liquid compound is [(Et3N)3-
A1]3'[(A1C13)6C13]3- which is prepared by mixing triethylamine and AlC13 to
form an
ionic salt complex precursor, REt3N)3-A1]3 [(C1)3]3- ; and complexing the
ionic salt
complex precursor with AlC13
The present disclosure also provides an ionic salt complex precursor
represented by
Formula (II)
[(Nit R2RAM inXj] n -
Formula II
wherein.
NR1R2R3 represents an amine,
RI, R2 and R3 are alkyl group or aryl group or H
Mt is a metal selected from the group consisting of Al, Fe, Zn, Mn and
Mg, Ti, Sn, Pd, Pt, Rh, Cu, Cr, Co, Ce, Ni, Ga, In, Sb, Zr and
combinations thereof,
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X is a halogen or a nitrate or a sulphate or sulfonate or carbonate or
phosphonate or acetate,
'n' represents 1 to 4,
T represents 1 to 6, and
`j 'represents I to 4,
The ionic salt complex precursor represented by Formula [(NR1R2R3)1M1Mir is
prepared by mixing an amine represented by Formula NR1R2R3 and a metal salt
represented by formula MIN. In one exemplary embodiment the ionic salt complex
precursor is [(Et3N)3-A1]31[(C1)3]3" which is prepared by mixing triethylamine
and
AlC13.
In one embodiment of the present disclosure, AlC13 used is in a hydrated form.
The present disclosure is further illustrated with the help of accompanying
drawings.
A process flow diagram for the preparation of the ionic salt complex precursor
is
illustrated in FIGURE 1. The process is carried out in either batch or semi-
continuous
or continuous mode.
In FIGURE 1 of the accompanying drawings,
(102) represents a pre-mixer; the pre-mixer can be either a batch or
continuous,
jacketed stirred vessel or static mixer or jet mixer or pump mixer;
(104) represents a reactor where ionic salt precursor formation takes place
between
amine and metal halide, the reactor (104) can be a jacketed stirred vessel,
static mixer,
slurry reactor or combinations thereof;
(106) represents a filter where the slurry obtained from (104) is filtered.
The filter
(106) can be a nutsche filter or pressure nutsche filter or centrifuge or
vacuum filter or
agitated nutsche filter or agitated nutsche filter and dryer;
(108) represents a dryer where the precursor is dried completely to remove the
residual solvent, the dryer (108) can be a tray dryer, column dryer, vacuum
drier,
agitated thin film dryer or a combination of a filter and a dryer such as an
agitated
nutsche filter and dryer;
(110) represents distillation system for the recovery of amine and solvent
from the
filtrate obtained from the filter (106). The distillation system (110) can be
a tray or
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bubble or packed bed distillation column where the recovery of amine and
solvent is
done separately as overhead and bottom products, alternatively the (110) can
also be a
falling film evaporator or an agitated thin film evaporator or combination of
a falling
film evaporator and an agitated thin film evaporator or single or multi effect
evaporator where amine and solvent are recovered as a same stream and recycled
back
to the pre-mixer (102);
In an embodiment AlC13 via stream 1 is mixed with a solvent stream 2 in the
pre-
mixer (102). The mixing can be either in a batch mode or continuous mode.
Initially
solvent may be charged followed by slow addition of a metal halide in a
continuous or
semi-continuous mode. The solvent includes but is not limited to ethyl
acetate,
ethanol, methanol, methyl iso butyl ketone, methyl ethyl ketone, benzene,
toluene,
dichloromethane and combinations thereof.
The weight to volume ratio of the metal halide to the solvent may vary from
1:0.5 to
1:10, preferably 1:5. The process can be carried out in the absence of a
solvent.
Chilled water or chilled brine is circulated inside the jacket in order to
remove heat
liberated in the pre-mixer. The pre-mixed feed is then transferred to a
reactor (104) via
stream 3. In the reactor (104) triethylamine is added via stream 4 either in a
semi
continuous mode or continuous mode. After addition, mixing time of 30 mins to
5 hrs
can be given in order to ensure complete ionic salt precursor formation.
In one embodiment the addition sequence can be changed i.e triethylamine via
stream
1 is mixed with a solvent stream 2 in the pre-mixer (102). The pre-mixed feed
is then
transferred to the reactor (104) via stream 3. In the reactor (104), AlC13 is
added via
stream 4 either in a semi continuous mode or continuous mode.
After the addition, mixing time of 30 mins to 5 hrs can be given in order to
ensure
complete ionic salt precursor formation.
The slurry mass is then transferred to the filter (106) via stream 5 where the
solids get
filtered off. These solids are transferred to the dryer (108) to get complete
dried ionic
salt precursor.
In one embodiment optionally a solvent wash may be given to the wet solid to
avoid
drying operation. The solvent includes but is not limited to benzene, toluene,
dichloromethane and the like.
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The filtrate obtained from (106) is subjected to distillation (110) via stream
14 where
amine and solvent are distilled off and recycled back to (104) and (102)
respectively.
Alternatively the stream 14 can be directly recycled to (102) without
distillation (110).
The residual solvent obtained from the dryer (108) is directly recycled to
(102) via
stream 8.
The ionic salt complex precursor is mixed with AlC13 to form the ionic liquid
compound
FIGURE 2 of the accompanying drawings illustrates a process flow diagram for
the
preparation of the ionic liquid compound/catalyst. The process is carried out
in either
a batch or semi-continuous or continuous mode.
In FIGURE 2 of the accompanying drawings,
(112) represents a second pre-mixer for mixing the dried ionic salt precursor
and
solvent in step, the pre-mixer (112) can be either a batch or continuous,
jacketed
stirred vessel or static mixer or jet mixer or pump mixer;
(114) represents a reactor where ionic liquid formation takes place from the
precursor
and metal halide, the reactor (114) can be a jacketed stirred vessel, static
mixer, slurry
reactor or combinations thereof.
In one embodiment the ionic salt precursor is transferred to the pre-mixer
(112) via
stream 9 where it is mixed with a suitable solvent which is transferred via
stream 10.
The ionic salt precursor utilized may be dried or solvent washed. The solvent
includes
but is not limited to benzene, toluene, dichloromethane and combinations
thereof.
The obtained slurry is then transferred to the reactor (114) via stream 11,
where A1C13
is added via stream 12 to the slurry to form ionic liquid. The addition of
AlC13 can be
continuous or semi-continuous. After addition, mixing time of 30 mins to 5 hrs
can be
given in order to ensure complete ionic liquid formation. This ionic liquid
compound/catalyst is then collected via stream 13.
In accordance with another aspect of the present disclosure there is provided
a process
for conducting at least one reaction selected from the group consisting of
alkylation
reaction, arylation reaction, acylation reaction, diels alder reaction and
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oligomerization reaction of at least one compound selected from the group
consisting
of C1 to C20 aliphatic compounds, C6 to Cg aromatic compounds and heteroaryl
compounds in the presence of an ionic liquid compound represented by formula
[(NRIR2R3);Mi]n+RM2Y01.
In one embodiment the reaction is carried out using at least one reactant
selected from
the group consisting of olefins, paraffins, alkyl or aryl halides, dialkyl or
diaryl
sulfates, dialkyl or diaryl carbonates, alcohols, carboxylic acids, esters,
thiols and
carbenes.
In one embodiment the reactant is olefin or a mixture of olefins having carbon
atoms
ranging from 2 to 50.
In accordance with the present disclosure the volume ratio of ionic liquid
compound
to the compound ranges from 0.01 to 1.5. The ionic liquid compound utilized is
selected from the group consisting of fresh ionic liquid compound, recycled
ionic
liquid compound and a combination thereof. The process further includes a step
of
recovering and recycling of said ionic liquid compound.
In accordance with one exemplary embodiment there is provided a process for
alkylation of benzene in the presence of an ionic liquid compound of the
present
disclosure and at least one alkylating agent to obtain linear alkyl benzene.
The
alkylation of benzene is carried out at a temperature of 20 to 100 C,
preferably at 30
to 60 C. The alkylating agent used is olefin selected from the group
consisting of Cio
to C14 olefins and mixtures thereof. Alternatively, the alkylating agent is a
mixture of
at least one C2 to C50 containing olefin and at least one C, to C50 containing
paraffin.
The ratio of benzene to the alkylating agent ranges from 1:1 to 20:1,
preferably, 6:1 to
10:1.
The alkylation of benzene is carried out at a pressure ranging from 1 to 10
atmospheres, preferably 1 to 6 atmospheres.
The process further includes recovering amine such as trialkylamine or triaryl
amine
from the used or deactivated ionic liquid.
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The alkylation process is illustrated herein below with the help of
accompanying
drawing (Fig. 3).
In FIGURE 3 of the accompanying drawings,
(116) represents a first mixer;
(118) represents a second mixer; the mixers M1 & M2 can be either a stirred
vessel or
plug flow reactor or static mixer or jet mixer or pump mixer or combinations
thereof;
(120) represents a first settler, the settler can be a gravity settling
vessel, either
horizontal or vertical, it can be a single step settling or a multi-step
settling with a
series of settlers, either horizontal or veitical;
(122) represents a third mixer which can be either a stirred vessel or static
mixer or jet
mixer or pump mixer;
(124) represents a second settler, it can be a gravity settling vessel, either
horizontal or
vertical, it can be a single step settling or a multi-step settling with a
series of settlers,
either horizontal or vertical;
optionally, there can be only one mixer (116) with one settler where the said
mixer
(116) can be either of the stirred vessel, static mixer, jet mixer and pump
mixer or two
mixers 116 & 118 with two settlers where the said mixers 116 & 118 can be a
stirred
vessel or static mixer or jet mixer or pump mixer and combinations thereof, or
optionally, another settler can be included between 116 & 118 if required;
(126) represents a purifier which can be a stirred vessel or centrifuge
separator or
packed column packed with alumina to remove acid traces;
(128) represents a third settler;
(132) represents a first fractionating column;
(134) represents a second fractionating column;
(136) represents a third fractionating column; and
(130) represents a catalyst recovery unit.
In one embodiment, a pre-mixed feed is prepared by mixing benzene and olefin
streams coming from lines 1 & 2 respectively. The pre-mixed feed is then fed
to the
mixer (116) where fresh/recycled/regenerated catalyst is added via line 3.
In another embodiment the catalyst (ionic liquid compound) and benzene can be
mixed in another pre-mixer and fed to the mixer (116).
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In one embodiment the olefin feed stream can be pure olefin, a mixture of
olefins and
paraffin's with carbon atoms ranging from 2-50, preferebly 10-15.
In another embodiment the mixed olefin stream contains 85-90 wt% paraffin's
and 10-
15 wt% olefins.
The alkylation reaction takes place in the mixer (116). The outlet of 116 is
directly fed
into second mixer (118) where further reaction takes place. The temperature
and
pressure conditions in 118 can be same as 116 or can be different. Optionally,
there
can be a settler between 116 & 118 where the reaction mixture from 116 can be
fed to
the settler and after the layer separation the upper hydrocarbon layer is
transferred to
118 along with a fresh catalyst and the lower catalyst layer can be recycled
to the
mixer 116/118 directly or through the catalyst recovery unit (130).
In a specific embodiment the olefin stream can be split and send
simultaneously to the
mixer 116 & 118 which gives an advantage of enhancing the mole ratio of
benzene to
olefin.
The outlet from 118 is fed into the settler (120) where hydrocarbon and
catalyst layers
are separated. The heavier catalyst layer from (120) via line 4 is recycled to
the mixer
116/122 directly or through the catalyst recovery unit (130). The upper layer
is
hydrocarbon layer which is fed to the mixer (122) via line 5 where
fresh/recycled/regenerated catalyst is added via line 3. The outlet from 122
is fed into
the settler (124) where hydrocarbon and catalyst layers are separated.
Optionally,
there can be only one mixer 116 instead of 116, 118 & 122 where the outlet of
116 is
fed into the settler (124) or optionally there can be two mixers 116 & 118
where the
outlet of 118 is fed into settler (124). The heavier catalyst layer from 124
via line 6 is
recycled to the mixer 116/122 through 130. The upper hydrocarbon layer is fed
to
hydrocarbon layer purifier (126) via line 7, where the deacidification of
hydrocarbon
layer takes place.
In a specific embodiment hydrocarbon layer is washed with either water or
alkali
solution via line 8 or directly centrifuged without any addition of water or
alkali
solution to remove trace acid content in the hydrocarbon layer.
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In one embodiment the volume ratio of water or alkali solution to hydrocarbon
layer is
in the range of 0.2 to 1 and the concentration of alkali may ranges from 2-50%
in
alkali solution.
In one embodiment the purifier (126) can also be a packed column filled with
alumina
base to remove acidic traces in hydrocarbon layer. In another embodiment the
purifier
can also be a stripper column where the acid traces will be removed by heating
the
hydrocarbon layer there by partial removal of benzene along with acid.
In another embodiment the said purifier can also be a combination of stripper
column
and packed column filled with alumina base or vice versa.
The outlet of 126 is directly fed to the settler (128) where layer separation
occurs. In
case of water or alkali wash the bottom layer will be aqueous layer with large
quantity, which is sent for effluent treatment via line 9 while in case of
centrifugation;õ
or crystallization, the bottom layer will be a catalyst layer with very small
qtAntity4
which is fed into (130) via line 9. The upper hydrocarbon layer from 128 is
fed into:
-
the fractionating column (132) where benzene is distilled off and recycled to
line! via -
line 11. The residue of 132 is fed to the fractionating column 134 via line 12
to
remove and recover paraffin via line 13. The residue of the fractionating
column (134)
is fed to the fractionating column (136) to separate linear alkyl benzene
product by
line 15 and heavy alkylated product by line 16.
In one embodiment the distillation columns 132, 134 & 136 can be operated
under.;
pressure or atmospheric pressure or under vacuum.
The process of the present disclosure is further illustrated herein below with
the help
of the following examples. The examples used herein are intended merely to
facilitate
an understanding of ways in which the embodiments herein may be practiced and
to
further enable those of skill in the art to practice the embodiments herein.
Accordingly, the examples should not be construed as limiting the scope of the
embodiments herein.
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EXAMPLE-1: Preparation of triethylamine- Aluminum chloride salt precursor
8.08 gm (0.061 mol) of AlC13 and 50 ml of ethyl acetate were charged into a
250 ml
RB flask under N2 atmosphere. Slowly under stirring, 18.4 gm (0.0182 mol) of
triethylamine was added for 30 minutes at 15-20 C to obtain a mass. The whole
mass
was then stirred for 4 hrs. The resultant mixture was then separated by
filtration. The
solids were washed with 100 ml fresh ethyl acetate followed by drying to get
22 gm of
triethylamine- Aluminum chloride salt precursor.
EXAMPLE-2: Preparation of Ionic liquid
15 gm (0.034 mol) of total solid powder obtained in the EXAMPLE-1 and 20 ml
benzene were charged into a 100 ml single neck RB flask kept on a magnetic
stirrer.
N2 flow was ensured inside the flask. The flask was kept in a water bath at 10-
15 C.
A magnetic needle was kept inside the flask for stirring. Slowly, 27.5 gm
(0.206 mol)
of AlC13 was added to the flask under stirring for 30 minutes. The obtained
mass was
stirred for 3-4 hrs. The resultant ionic liquid was kept under closed
conditions.
EXAMPLE-3: Preparation of Ionic liquid
15 gm (0.034 mol) of total solid powder obtained in the EXAMPLE-1 was charged
into a 100 ml single neck RB flask kept under overhead stirrer. N2 flow was
ensured
inside the flask. The flask was kept in a water bath at 10-15 C. Slowly,
under stirring
29.3 gm (0.21 mol) of A1C13 was added to the flask under stirring for 30
minutes. The
obtained mass was stirred for 3-4 hrs. The resultant ionic liquid was kept
under closed
conditions.
EXAMPLE-4: Alkylation reaction
52.02 litres of hydrocarbon stream containing 10-13% C10-C14 olefins & 87-90%
paraffins and 20.02 litres of benzene were charged into a 250 L glass reactor
kept
under an overhead stirrer, placed in a heating mantle. N2 flow was ensured
inside the
reactor. The reactor was then heated to 38-39 C. Once the temperature was
achieved,
0.7 kg of the ionic liquid catalyst prepared as per EXAMPLE-2 was added to the
reactor and stirred for 5 minutes. After 5 minutes the reaction mass was
allowed to
settle for 10 minutes. The layers were then separated. The upper hydrocarbon
layer
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was then analysed. The conversion of benzene to linear alkyl benzene was found
to be
99.7%.
EXAMPLE-5
The lower catalyst layer obtained from EXAMPLE-4 was recycled with fresh
hydrocarbon stream and benzene as per the procedure provided in EXAMPLE-3. The
conversion of benzene to linear alkyl benzene was found to be 99.7%.
EXAMPLE-6: Alkylation reaction
141.5 ml (124.3 gm) of benzene was added to a 250 ml RB flask kept under an
overhead stirrer under N2 atm. 7.5 gm of ionic liquid catalyst prepared as per
EXAMPLE-2 was added to the flask. 23.4 ml benzyl chloride was added to flask
at
45-46 C and stirred for 15 min. After completion of reaction, catalyst and
hydrocarbon layers were separated. The upper hydrocarbon layer was then
analysed
by gas chromatography for benzyl chloride conversion. The conversion of benzyl
chloride to biphenyl methane was found 90%.
EXAMPLE-7
The lower catalyst layer obtained from EXAMPLE-6 was recycled with fresh
benzene
and benzyl chloride as per the procedure provided in EXAMPLE-6. The conversion
of
benzyl chloride was found 90%.
EXAMPLE-8: Oligomerization
100 mL of hydrocarbon stream containing 10-13% CIO-C14 olefins and 87-90%
paraffins were charged into a 250 InL glass reactor kept under an overhead
stirrer,
placed in a heating mantle. N2 flow was ensured inside the reactor. The
reactor was
then heated to 45 C. Once the temperature was achieved, 0.1 g of the ionic
liquid
catalyst prepared as per EXAMPLE-2 was added to the reactor and stirred for 10
minutes. After 10 minutes the reaction mass was allowed to settle for 10
minutes. The
layers were then separated. The upper hydrocarbon layer was then analysed. The
conversion of olefins was found to be 96.15%.
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EXAMPLE-9: Alkylation of Phenol
23.5 g of Phenol and 2.2 g Methyl tert-butyl ether (MTBE) were charged into a
100
mL glass reactor kept under an overhead stirrer, placed in a heating mantle.
N2 flow
was ensured inside the reactor. The reactor was then heated to 60 C. Once the
temperature was achieved, 0.25 g of the ionic liquid catalyst prepared as per
EXAMPLE-2 was added to the reactor and stirred for 3 hrs. After 3 hrs the
reaction
was workup with 25 mL distilled water. The conversion of MTBE was found to be
95%.
EXAMPLE-10: Diels Alder reaction
2.76 g of Isoprene and 1.02 g Vinyl Acetate were charged into a 100 mL glass
reactor
kept under an overhead stirrer, placed in a heating mantle. N2 flow was
ensured inside
the reactor. The reactor was then heated to 60 C. Once the temperature was
achieved,
0.03 g of the ionic liquid catalyst prepared as per EXAMPLE-2 was added to the
reactor and stirred for 4 hrs. After 4 hrs the reaction was workup with 10 mL
ethyl
acetate. The conversion of reactants was found to be 98%.
EXAMPLE-11: Acylation of Benzene by Acetyl Chloride
19.5 g of Benzene and 3.5 g Acetyl Chloride were charged into a 100 mL glass
reactor
kept under an overhead stirrer, placed in a heating mantle. N2 flow was
ensured inside
the reactor. The reactor was then heated to 60 C. Once the temperature was
achieved,
0.21 g of the ionic liquid catalyst prepared as per EXAMPLE-2 was added to the
reactor and stirred for 2 hrs. After 2 hrs the reaction was workup with 25 mL
distilled
water. The conversion of Acetyl Chloride was found to be 98%.
EXAMPLE-12: Acylation of Benzene by Benzoyl Chloride
19.5 g of Benzene and 1.95 g Benzoyl Chloride were charged into a 100 mL glass
reactor kept under an overhead stirrer, placed in a heating mantle. N2 flow
was
ensured inside the reactor. The reactor was then heated to 60 C. Once the
temperature
was achieved, 0.21 g of the ionic liquid catalyst prepared as per EXAMPLE-2
was
added to the reactor and stirred for 3 hrs. the reaction was workup with 15 mL
distilled water & 15 mL ethyl acetate. The conversion of Benzoyl Chloride was
found
to be 90%.
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EXAMPLE-13: Synthesis of A1C13-TEA/ ZnC12 Ionic Liquid
g of AlC13-TEA ionic salt precursor was charged into a 100 mL glass reactor
kept
under an overhead stirrer, placed in a water bath. Then, 18.66 g Zinc Chloride
was
slowly added in to it with constant stirring. N2 flow was ensured inside the
reactor.
The mixture was stirred for 3 hrs to get viscous ionic liquid.
EXAMPLE-14: Synthesis of SbC13- FLA/ FeC13 Ionic Liquid
22.5 g of SbC13 and 100 mL ethanol were charged into a 250 mL glass reactor
kept
under an overhead stirrer, placed in a water bath. Then, 36 g TEA was slowly
added in
to it with constant stirring. N2 flow was ensured inside the reactor. The
mixture was
stirred for 4 hrs to get white coloured solid. The reaction mass was allowed
to settle
for 10 minutes. The solid was then separated and dried at 100 C.
10 g of SbC13-TEA ionic salt precursor was charged into a 100 mL glass reactor
kept
under an overhead stirrer, placed in a water bath. Then, 18.31 g FeC13 was
slowly
added in to it with constant stirring. N2 flow was ensured inside the reactor.
The
mixture was stirred for 3 hrs to get viscous ionic liquid.
Throughout this specification the word "comprise", or variations such as
"comprises"
or "comprising", will be understood to imply the inclusion of a stated
element, integer
or step, or group of elements, integers or steps, but not the exclusion of any
other
element, integer or step, or group of elements, integers or steps.
The use of the expression "at least" or "at least one" suggests the use of one
or more
elements or ingredients or quantities, as the use may be in the embodiment of
the
disclosure to achieve one or more of the desired objects or results.
Any discussion of documents, acts, materials, devices, articles or the like
that has been
included in this specification is solely for the purpose of providing a
context for the
disclosure. It is not to be taken as an admission that any or all of these
matters form a
part of the prior art base or were common general knowledge in the field
relevant to
the disclosure as it existed anywhere before the priority date of this
application.
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The numerical values mentioned for the various physical parameters, dimensions
or
quantities are only approximations and it is envisaged that the values
higher/lower
than the numerical values assigned to the parameters, dimensions or quantities
fall
within the scope of the disclosure, unless there is a statement in the
specification
specific to the contrary.
While considerable emphasis has been placed herein on the specific features of
the
preferred embodiment, it will be appreciated that many additional features can
be
added and that many changes can be made in the preferred embodiment without
departing from the principles of the disclosure. These and other changes in
the
preferred embodiment of the disclosure will be apparent to those skilled in
the art
from the disclosure herein, whereby it is to be distinctly understood that the
foregoing
descriptive matter is to be interpreted merely as illustrative of the
disclosure and not as
a limitation.
